Cyclic adsorption process



Filed ndv. 25,1956

' Julyfl's, 1957* E. B. MILLER CYCLIC ADSORPTION PROCESS 6 Sheets-Sheet1` Qi, mhwmkw v ATTORNEY l 'July 16,1957 E. B. MILLER v2,799,364 1CYCLIC ADSORPTION PROCESS Filed NOV. 25, 1956 -6 Sheets-Sheet 2INVENTQR. [RA/55T a man@ ATTORNEYS July 16, 1957 E. B. MILLER CYCLICADS'ORPTION PROCESS e Sheets-sheet 4 Filed Nov. 23, 1956 I NVENTORATTORNEYS July 16, 1957 E. B. MlLLER 2,799,364

YcpIc ADsoRPTIoN PROCESS Filed Nov. 23, 1956 6 Sheets-Sheet 5 ATTORNEYSE. B. MILLER CYCLIC ADSORPTION PROCESS July 16, 19.57

6 Sheets-Shes?I 6 Filed Nov. 255, 1956 FIG. Il.

INVENTOR ERA/[57" 5. /V/-ER ATTORNEYS a t 2,799,364 Patented July 16,1957 2,799,364 CYCLIC ADSORPTION PROCESS Ernest B. Miller, Houston,Tex., assignor to .leierson Lake Sulphur Company, New Orleans, isa., acorporation of New Jersey Application November 23, 1956, Serial No.623,862 4 Claims. (Cl. 18S-114.2)

This invention relates to gas dehydrating and has more particularreference to a continuous process for removing moisture and condensablehydrocarbons from wet natural gas at the source, prior to thetransmission thereof through pipe lines, and recovering the condensablehydrocarbons.

One object of the present invention is to provide a novel and improvedcyclic adsorption process for dehydrating wet natural gas of the typecomprising an adsorption cycle in which the natural gas being treatedpasses through one or more adsorption stages of the adsorber; and anactivation cycle employing a captive activation gas recycledthrough aheater, the activation stage of the adsorber, and a condenser separator.

Another object of the present invention is to provide a novel andimproved cyclic Aadsorption process for the removal and/ or recovery ofwater vapor and condensable hydrocarbons from wet natural gas ascharacterized above including three purging cycles, a irst purging cyclepreceding the activation cycle and second and third purging cyclesfollowing in succession after the activation cycle so as to permit ahigh concentration of desorbed products in the recycling captiveactivation gas by preventing the dilution of the activation gasbyslippage gas and also preventing the loss of desorbed products byslippage of the activation gas into the outgoing eluent stripped naturalgas.

Another object of the present invention is to provide a novel andimproved adsorption process for recovering condensable hydrocarbons fromwet natural gas as characterized above, which is characterized bymaintaining at least one bed of adsorbent material in each of aplurality of stages; continuously heating and recycling captiveactivation gas through at least one of said stages to vaporize themoisture and condensable hydrocarbons contained in the adsorbentmaterial therein; continuously directing a flow of a first purgingmedium through at least another one of said stages to purge the stage;continuously directing a flow of a second purging medium through .atleast another one of said stages to purge the stage; continuouslydirecting the flow of the natural gas to be treated through theremainder of said stages so that the contained water vapor andcondensable hydrocarbons will be adsorbed by the adsorbent materialtherein; periodically shifting the relative position of the particularadsorbent beds and the particular flow of uids in each of said stages sothat each stage becomes, in succession, a iirst purging stage, anactivation stage, a second purging stage and an adsorption stage;continuously directing the flow of the effluent fluid from the secondpurging stage into the iirst purging stage for use as the iirst purgingmedium and continuously diverting a portion of the flow of the strippedeluent fluid from the last adsorption stage for use as the secondpurging medium; continuously directing the effluent iluid from the firstpurging stage back into the ow ofthe fluid being treated on its way tothe adsorber; continuously directing the flow of the recyclingactivation gas, after its passage through the activation stage, througha condensing and separating zone, and there condensing and recoveringthe water and condensable hydrocarbons and continuously directing the owof the stripped activation gas back into the recycling path. i

Other objects and advantages of the invention will appear in thefollowing specification when considered in connection with theaccompanying drawings, in which:

Fig. l is a schematic view showing one embodiment of apparatus and thearrangement thereof for carrying out the method of the present inventionand the flow of the various fluids therethrough;y

Fig. 2 is a side elevational view of the adsorber shown in Fig. l;

Fig. 3 is a plan view of the apparatus'shown in Fig. 2;

Fig. 4 is a vertical sectional view taken on the line 4-4 of Fig. 3, butomitting the driving apparatus;

Fig. 5 is a horizontal sectional view taken on the line 5-5 of Fig. 4;

Fig. 6 is a fragmentary sectional view taken on the line 6 6 of Fig. 4,showing the manner of bracing the upper ends of the elongated adsorbentmaterial containing vessels;

Fig. 7 is a fragmentary sectional view taken on the line '7--7 of Fig.4, showing the manner of supporting the lower ends of the elongatedadsorbent material containing vessels; v

Fig. 8 is a horizontal sectional view taken on the line 8 8 of Fig. 4;

Fig. 9 is a detail sectional view, taken on the line 9-9 of Fig. 8;

Fig. l() is a vertical sectional view, with parts broken away, of theadsorbent material containing vessels shown in Fig. 4, showing thecontainers for holding the adsorbent material mounted therein; and

Fig. l1 is a plan view ofthe container shown in Fig. 10.

The present invention isl drawn to a novel method of dehydrating wetnatural gas under high pressure and removing the condensablehydrocarbons therefrom and is an improvement over the method disclosedand claimed in my co-pending application Ser. No. 619,375, led October19, 1956, for Cyclic Adsorption Process.

The present invention provides a novel and improved process forVremoving and/or recovering water vapor and condensable hydrocarbonsfrom wet natural gas. The process is a continuous cyclic adsorptionprocess employing an adsorber in which at least one bed of adsorbenmaterial is maintained in a plurality of stages and, in general,comprises an adsorption cycle in which a continuous ow of the naturalgas being treated is directed, under high pressure, through one or, moreadsorption stages so that the contained water vapor and condensablehydrocarbonswill be adsorbed by the beds of adsorbent material in theadsorption stages; an activation cycle in which a flow of a captiveactivation Inedium, under high pressure, is continuously recirculatedthrough a heater; an activation stage to vaporize the moisture andcondensable hydrocarbons contained in the adsorbent material therein; aplurality of purging cycles to prevent dilution of the recyclingactivation medium, including a first purging cycle in which theAeffluent iluid from a second purging cycle is continuously passed intoa purging stage immediately preceding the activation stage, called thefirst purging stage, with the eflluent uid from the first purging stagepassing into the flow of the fluid being treated on its way to the firstadsorption stage, and a second purging cycle in which a portion of theeluent stripped uid from the last adsorption stage is..

continuously diverted and passed into a purging stage immediatelyfollowing the activation stage, called the second purging stage, withthe effluent `iuid from the secgreased ond purging stage passing intothe first purging stage; the p erlodical shifting of the relativepositions of the particular adsorbent material and the particular iiowof uid through each stage, either by moving the beds successlvelythrough the stages or by shifting the flows of fluid through the severalstages, so that each stage becomes in succession, a first purging stage,an activation stage, a second purging stage and an adsorption stage; anda product recovery cycle in which the flow of the recycling activationgas, after its passage through the activation stage passes through acondensing and separating zone where the water vapor and condensablehydrocarbons are condensed and recovered with the stripped activationgas from the condensing and separating zone passing back into itsrecycling path.

While any suitable usual type of adsorption apparatus may be employedto'practice the process of the present invention, for purpose ofillustration, the process will be described as carried out by employinga rotary type or" adsorber in which a plurality of elongated uprightclosed vessels containing adsorbent material are rotated directly insuccession and substantially continuously through the various stages ofthe adsorber.

Referring now to the drawings, there is shown, in Fig4 1, one embodimentof apparatus and arrangement thereof for carrying out the method of thepresent invention. The apparatus shown includes a seven stage rotaryadsorber 1, three stages of which are employed as adsorption stages,three stages of which are employed as purging stages, and one stage ofwhich is employed as an activation stage; a pair of intercoolers 2 and 2employed to cool the gas being treated between the adsorption stages; aheater 3 employed to heat the activation gas used in the activationstage; a fan or blower 4 for recirculating the activation gas throughthe activation stage; a condenserseparator 5 employed to condense themoisture and condensable hydrocarbons contained in the recirculatingactivation gas after it has passed through the activation stage of theadsorber; and a suction fan or blower 4' for pulling the purging mediumthrough the purging stages of the adsorber.

The wet gas being treated is delivered, at high pressure, from the usualcompressor or source of supply (not shown) to the first adsorption stageof the adsorber by means of a pipe line 6. The gas passes through thefirst adsorption stage where some of the moisture and condensablehydrocarbons are removed. From the first adsorption stage of theadsorber, the gas passes through pipe line 7 and intercooler 2 to thesecond adsorption stage of the adsorber. After passing through thesecond adsorption stage, where additional moisture and condensablehydrocarbons are removed, the gas passes through pipe line 8 andintercooler 2 to the third adsorption stage of the adsorber. Afterpassing through the third adsorption stage the moisture and condensablehydrocarbon stripped gas passes through pipe line 9 to its variouspoints of use.

The captive activation gas is heated in the heater 3 to a temperature offrom 300 F. to 600 F., depending upon the moisture content of the gas tobe treated and the type of hydrocarbons to be recovered, and, from theheater, passes through a pipe line 10 to the activation stage of theadsorbed. The heated gas passes upwardly through the activation stage ofthe adsorber, desorbing the accumulated moisture and hydrocarbons fromthe adsorbent material therein. The heated gas and the moisture andcondensable hydrocarbons desorbed from the adsorbent material passthrough a pipe line 11 to the condenser-separator 5, where the moistureand condensable hydrocarbons are condensed and separated. The water andcondensable hydrocarbons are drained from the bottom of the separator bymeans of a suitable drain line.

From the condenser-separator 5, the now stripped activation gas passesthrough a pipe line 12 to the fan or blower d and is recirculated by theblower through a pipe line :t3 and the heater 3 back through theactivation stage of the adsorber. This recirculation process iscontinuous.

The captive stream of gas in the activation system is cireuiated bymeans of the blower 4 through the heater 3, the activation stage of theadsorber and the condenserseparator 5. The composition of this streamwill build up gradually in terms of condensable vapors, composed chieiyof hydrocarbons, until the dew point of the captive gas stream reachescondenser temperature, and will, thereafter, yield as liquids all thecondensable vapors deso-rbed in the activation stage of the adsorber.

The vessels which contain the adsorbent beds are rotated so that eachvessel passes in succession through the various stages of the adsorber.As the vessels move through each stage they are filled with theparticular gas tiowing through the stage and carry this gas into thenext or succeeding stage in their rotary movement. This carrying of gasfrom one stage to the other by the vessels is called slippage.

In order to prevent slippage gas from the first adsorption stage, whichwould consist of the raw gas being treated, from being carried over intothe activation stage and diluting the recycling activation gas, apurging stage is interposed between the first adsorption stage and theactivation stage and called the first purging stage.

Also, in order to prevent the slippage gas from the activation stage,which is rich in condensable hydrocarbons, from being carried over intothe third adsorption stage, where it would pass out of the adsorber withthe outgoing stripped gas, two purging stages are interposed between theactivation stage and the third adsorption stage, called the secondpurging stage and the third purging stage.

The effluent gas from the second purging stage, which consists chieiiyof slippage activation gas, is used as the purging medium for the firstpurging stage and passes from the second purging stage through a pipeline 14 into the tirst purging stage. The effluent gas from the firstpurging stage passes through a pipe line 15 to the suction fan or blower4 and is discharged from the blower 4 through pipe line 16 back intopipe line 6 to join the ow of the raw gas being treated on its way tothe first adsorption stage of the adsorber.

As the gas used as the purging gas in the first purging stage consistssubstantially of slippage activation gas, the slippage gas from the rstpurging stage into the activation stage would consist substantially ofactivation gas, so that the recycling captive activation gas would notbe diluted.

A portion of the efiiuent stripped raw gas flowing from the thirdadsorption stage of the adsorber through pipe line 9, is diverted foruse as the purging medium for the second and third purging stages andpasses through pipe lines i7 and 17 into the second and third purgingstages, respectively, of the adsorber. The eiuent gas from the secondpurging stage, as above stated, pushes the slippage gas from theactivation stage through pipe line 14 into the first purging stage. Theefiiuent gas from the third purging stage pushes the slippage gas fromthe second purging stage through pipe line 18 into pipe line 15, thentothe suction blower 4' and through the pipe line 16 back into pipe line6, where it joins the ow of the raw gas being treated on its way to thefirst adsorption stage of the adsorber.

The employment of the three purging stages, as above outlined, providesfor complete purging of the adsorbent material while preventing dilutionof the activation gas and reduces loss of condensable hydrocarbons byslippage, thus greatly increasing the eiciency and operation of theadsorber. In addition, the use of the three purging steps, as outlinedabove, including the-use of the suction blower 4 to pull the ow of gasesthrough the three purgingV stages, permits the pressure differential inthe various stages to be controlled, thus reducing leakage across theseals between the stages.

Also, in order to prevent an undue build up of pressure `within theactivation stage of the adsorber, a valved pipe line 19 may be employedto connect pipe line 10 of the recycling activation system to pipe line14 through which the purging'medium for the first purging stage passesinto the first purging stage. in the pipe line 19, the pressure build upin the activation stage may be properly controlled.

While any suitable type of rotary adsorber may be cmployed to practicethe method of the present invention, the adsorber illustrated isgenerally similar to the uid treating apparatus shown in my Patent No.2,751,033, issued .Tune 19, 1956, for Fluid Treating Apparatus.

As shown in Figs. 2 to l1, inclusive, the adsorber comprises anelongated upright cylindrical pressure vessel 20 having anged verticallyaligned circular openings 21, 22 in its top and bottom walls,respectively, closed by top and bottom flanged cover plates 23, 24removably secured to cover said openings, as by bolting; suitableframework, indicated at 25, for supporting the vessel 20 in an uprightposition, a rotatable vertical shaft 26 extending through the pressurevessel 20 with its upper end journaled ina suitable cap bearing carriedby the upper closure member 23 and with its lower end extending througha suitable shaft seal, secured to the bottom of the lower closure member24; a vertical shaft 27 coupled to the bottom end of the shaft 26 andconnected to suitable differential gearing, indicated at 28, driven by amotor 29; a support disc 30 fixedly mounted on the shaft 26 for rotationtherewith within said pressure vessel and providing support for aplurality of elongated fluid treating material containing cylindricalvessels 31; upper and lower distributive assemblages, indicatedgenerally at 32, 33, each assemblage comprising an annular stationarymember 34 having a plurality of compartments or manifolds formedtherein, a tube sheet disc valve 35 slidably mounted on the shaft 26 forrotation therewith, a spring support disc 36 lixedly mounted on theshaft 26 and supporting a plurality of coiled springs 37 which engagethe tube sheet disc valve 35 and tightly press it against the open endof the annular stationary member 34; a plurality of flexible pipes 38,each connecting the upper end portion of one of the vessels 31 and thetube sheet disc valve 35 of the upper distributive assemblage; aplurality of flexible pipes 39, each connecting the lower Lend portionof one of the vessels 31 and the tube sheet disc valve 3S of the lowerdistributive assemblage, a plurality of inlet-outlet conduits, sevensuch being shown, 4t), 41, 42, 43, 44, 45 and 46, connected to `theannular stationary member 34 of the upper distributive assemblage andextending upwardly through the upper cap closure member 23, for theingress and egress of fluids to and from the upper stationary member 34;and a plurality of inlet-outlet conduits, seven such being shown, 40',41', 42', 43', 44', 45' and 46', connected to the annular stationarymember 34 of the lower distributive assemblage and extending downwardlythrough the lower cap closure member 24 for the ingress and egress offluids to and from the lower stationary member 34.

The cylindrical pressure vessel 20 and the cap cover members 23, 24 arepreferably made of heavy boiler plate. The flanges formed on theperipheries of the openings 21, 22 of the vessel 20 and the peripheriesof the cap cover members 23, 24 are preferably formed of heavy ironrings, rectangular in cross section and are welded to the peripheraledges of the openings and the cover plates, as indicated at 47.

The shafting 26, preferably and as shown, is formed of three sections,an upper section 43, an intermediate section 49, and a lower or bottomsection 50. The upper and lower sections 48 and 50 consist of solid rod,round in cross section. The intermediate section 49 consists of a hollowpipe having an internal diameter considerably larger than therdiametersof the upper and lower sections.

By proper regulation of the valve o 6 The upper section 48 has its upperend journaled l in a suitable cap bearing 51 carried by the upper covermem-4 ber 23 and its'lower end supported in a support bushing 52 mountedin the upper end of the intermediate section 49 with a pin 53 passingthrough the two'sections and the bushing for rigidly and detachablysecuring the two sections together. 4

- The bottom section has its upper end engaged in a support bushing 54mounted in the lower end of the intermediate section 49 with a pin 55passing through the two sections and the bushing for rigidly anddetachably securing the two sections together, and with its lower endex` tending through the lower cover member 24 and a suitable shaft seal56 and coupled to the upper end of the shaft 27. The support disc 30which supports the cylindrical vessels 31 is composed of twosemi-annular at pieces l57, the inner adjacent straight edges of whichare providedV with anges which are bolted together tok form the com-Aplete disc. This is to permit of assembling the disc with#Y in thepressure vessel 20.

The disc 30 (see Figs. 4 and 7) isfxedly secured, as" by bolting, to acollar 58 fixedly secured to the intermediate section 49 of the shaft26, so that the disc will rotate with the shaft. The outer peripheraledge por-y tion of the disc 30 is supported by means of a plurality ofsupporting links or arms 59, each having its upper end bolted to one ofa plurality of circumferentially spaced lugs 60 carriedV by a collar 61xedly secured to the intermediate section 49 of the shaft 26 and itslower end bolted to one of a plurality of circumferentially spacedupstanding lugs 62 secured to the upper surface of the disc 30.

The vessels 31 are supported by the disc 30, as by means of a pluralityof supporting links or arms 634 in the form of short sections ofstructural angles, each arm 63` having its outer end portion xedlysecured to the bottom and one side of one of said vessels 31, as bywelding, and its inner end portion fixedly secured, as by bolting, toone of a plurality of circumferentially yspaced dependent lugs 64, inthe form of short sections of I-beams, welded to the under surface ofthe disc 30 (see Figs. 4 and 7).

Means may be provided for holding the cylindrical vessels 31 in theirupright position `encircling the shaft 276. In the particular embodimentofthe invention illustrated, such means are shown as comprising a disc65 composed of two semi-annular flat pieces 66, 66, the inner adjacentstraight edges of which are providedwith anges which are bolted togetherto form the complete disc. This is to permit of assembling the discwithin the pressure vessel 20. The disc 65 (see Figs. 4 and 6) is xedlysecured,Y as by bolting, to a collar 67 iixedly secured totheintermediate section 49 of the shaft 26, so that the disc will rotatewith the shaft. The upper end portionsof the vessels 31 are held intheir upright position by the disc 65, as by means of a plurality ofbracing strips or arms 68 in the form of short sections of structuralangles. Each arm 68 has its outer end bolted to a lug 69 welded on theouter surface of one of the vessels 31 and its inner end portion xedlysecured, as by bolting, to the upper surface ofthe disc 65. Y

The upper and lower distributive assemblages 32, 33 are identical inconstruction and, as shown in Fig. 4, each comprises an annulartrough-shaped stationary member 34 having a plurality of compartments ormanifolds formed therein; a tube sheet disc valve 35 slidably mounted onthe shaft 26 for rotation therewith; and a spring support disc 36fixedly mounted on the shaft 26 andv supporting a plurality of coiledsprings 37 which engage the tube sheet disc valve 35 and tightly pressit against the open end of the annular stationary menu identical inconstruction and,as shown in Figs. 4, 5, A8 and- 9, each isk formed inthe shape of an annular trough '7 having an annular top (or bottom) wall70 and annular side walls 71, 72 (see Figs. 4 and 9).

The member 34 is divided into a plurality of compartments or manifolds,as by means of a plurality of circumferentially spaced pairs of wallmembers 73 extending transversely of the member 34 and having their top(vor bottom) and side walls welded to the top (bottom) and side walls ofthe member 34 to form gastight joints. Seven such compartments ormanifolds are shown and, for the purposes of clarity of description,designated manifolds a, b, c, d, e, f and g, respectively, see Fig. 8.

The upper member 34 of the upper distributive assemblage 32 is heldstationary relative to the rotation of the shaft 26 and the upper tubesheet disck valve 35 by the upper inlet-outlet conduits 40, 41, 42, 43,44, 45, and 46, which are welded to the upper cap closure member 23 andhave their lower ends connected, as by welding, to the manifolds a, b,c, d, e, f and g, respectively, in the upper member 34 to providecommunication therewith.

The lower member 34 of the lower distributive assemblage is heldstationary relative to the rotation of the shaft 26 and the lower tubesheet disc valve 35 by the lower inlet-outlet conduits 40', 41', 42',43', 44', 45', and 46', which are welded to the lower cap closure 24 andhave their upper ends connected, as by welding, to

the manifolds a, b, c, d, e, f, and g, respectively, in the lower member34 to provide communication therewith.

The upper and lower tube sheet disc valves 35 are identical inconstruction and, as shown in Fig. 4, each comprises a flat metal dischaving a plurality of circumferentially spaced circular openings 74formed in a circular row adjacent its periphery. The disc is providedwith a collar 75 having a plurality of radially extending reinforcingribs welded to its bottom surface or cast integral therewith. The collar75 is keyed on the upper (lower) section of the shaft 26 to havelongitudinal movement therealong as well as rotative movement therewith,as by means of a set screw 76 slidably eni gaging in a longitudinalgroove 77 formed in the upper (lower) section of the shaft 26. A secondcollar 78 is xedly secured to the shaft 26 immediately beneath thecollar 75 to limit the inward movement of the disc as it moveslongitudinally of the shaft 26. The disc 35, as well as the collar 75,are loosely tted on the shaft 26 so that the disc valve can be movedslightly to conform to anyl change in the plane of the engaged surfaceof the .stationary member 34, due to unequal expansion and contraction.

The tube sheet disc 35 is so mounted on the shaft 26 that it slidablyengages the open bottom (top) end of the annular stationary member 34with the circular row of openings 74 vertically aligned with themanifolds a, b, c, d, e, f and g, so that each manifold will be incommunciation with a group of the circular openings.

The upper and lower spring support discs 36 are identical inconstruction and, as shown in Fig. 4, each comprises a metal discmounted on the shaft and having a hub 79 provided with a plurality ofcircumferentially spaced radial ribs or webs welded to the under face ofthe disc to strengthen it. The hub is xedly secured to the shaft, as bya set screw. A plurality of vertically extending circumferentiallyspaced coiled springs 37 are interposed between the tube sheet discvalve 35 and the spring support disc 36, In order to insure that thesprings 37 remain in proper position, they are mounted on'and betweenshort stubs StB extending upwardly from the disc 36 and shortcorresponding stubs 80' extending downwardly from the disc 35. Theconstruction and arrangement is such that the springs 37 will keep thedisc valve 35 evenly and firmly pressed into engagement with the undersurfacevof the annular stationary member; l34.

The vupper, and lower exible pipes 3S, 39, which conneet the upper andlower end portions of the adsorbent material containing vessels 31 tothe upper and lower distributive assemblages are identical inconstruction and, as shown in Figs. 4 and 10, each comprises a thinwalled cylindrical metal tube having the greater portion of its wallformed in a sinuous shape to give it flexibility, the outer cylindricalend of each tube is detachably secured to a nozzle Si formed on theupper (lower) end portion of the vessel 31, as by strapping. Thecylindrical inner end of the tube is provided with an integral flange82. The opening in the cylindrical inner end of the tube is aligned withone of the circular openings 74 formed in the upper (lower) tube sheetdisc valve 35 and the ange 32 is detachably secured to the outer surfaceof the disc valve. as by countersunk bolts, so that the inner surfaceofthe disc wall will be smooth and uninterrupted (see Fig. 4).

To prevent the escape of gas between the rotating tube sheet disc valve35 and the manifolds in the member 34, sealing ring gaskets 83 areplaced at the juncture of the side walls of the member 34 and the discvalve 35. The ring gaskets 83 are wedged into annular troughs 84,secured, as by welding, to the outer surface of the side walls of themember 34. Each trough comprises an annular' top (bottom) wall 85 and anannular side wall 86. The ring gaskets 83, preferably and as shown,comprise a plurality of annular strips of packing, generally rectangularin cross section and made of any suitable material, such as Teiion orsilica impregnated asbestos.

rEhe seven manifolds a, b, c, d, e, f and g are sealed off from eachother by means of cross seals 87, each sealed into a recess 88 formed bythe adjacent end walls of the manifolds and a bottom plate S9 verticallyspaced from the open end of the manifolds (see Figs. 8 and 9). Eachcross seal is tightly wedged in its recess with its outer ends in tightengagement with the adjacent side walls of the annular seals S3 and withits bottom surface in sealing engagement with the upper (lower) surfaceof the tube sheet disc. ln order for the outer ends of the cross sealsto engage the adjacent side walls of the annular seals 83, the portionsof the side walls 71 and 72 of the member 34 which extend between eachpair of adjacent transverse members 73 are cut away, as indicated at 90,for a distance equal to the thickness of the seals 83 (see Fig. 9).

The widths of the manifolds a, b, c, d, e, j and g are substantially thesame as the internal diameters of the circular openings 74 in the tubesheet disc 35, so that each cross seal can electively seal olf one ofthe openings.

Each of the openings 74 formed in the upper tube sheet disc 35 is invertical alignment with a corresponding one of the openings 74 formed inthe lower tube sheet disc 35 and each of the cross seals 87 whichseparate the manifolds a, b, c, d, e, f and g formed in the upperstationary member 34 is in vertical alignment with a corresponding oneof the cross seals 87 which separate the manifolds a, b, c, d, e, f andg formed in `the lower stationary member 34.

When the rotary disc valves 35 and the vessels 31 are stationary, theforegoing arrangement, in effect, divides the adsorbent materialcontaining vessels 31 into seven groups, with one group connected tocommunicate with the manifolds a, one group connected to communicatewith the manifolds b, one group connected with the manifolds c, and onegroup connected to communicate with the manifolds d, one group connectedto communicate with the manifolds e, one group connected to communicatewith the manifolds f, and one group connected to communicate with themanifolds g. Each group of vessels Sl, together with the upper and lowermanifolds with which they are incommunication form separate ow passagesthrough the adsorber so that seven separate, distinct and continuousflows of iiuid may pass through the apparatus. Each ow entering theupper distributive 2,799,364 I y A assemblage by means of one of theinlet-outlet conduits 40, 41, 42, 43, 44, 45, or 46, thence through oneof the groups `of vessels 31 into the lower distributive assemblage andout through one of the inlet-outlet conduits 40', 41', 42', 43', 44',45', or 46. As the vessels 31 and the upper and lower disc valves 35rotate, each of the flows of fluid will successively pass through thevessels 31. For convenience in description, each ow passage is called astage, in which either adsorption, activation, or purging takes place,depending upon the particular fluid flowing therethrough. Also, thevessels 31 are called zones, in which either adsorption, activation orpurging takes place, depending upon the particular fluid flowingtherethrough at a given time.

The silica gel containing vessels 31 are identical in construction and,as shown in Figs. l and 1l, each cornprises an elongated hollow tubularmember 91 having a closed bottom end and an open upper end provided witha flanged collar 92 to which is secured, as by bolting, a removablecover plate 93.

A horizontally disposed annular disc 94 is mounted in the lower endportion of the member 91 and secured therein, as by welding, to form agas-tight joint between the outer peripheral edge of the disc and theside Wall of the member 91. The lower annular disc 94 forms a supportfor an elongated annular fluid treating material container 95. Thecontainer 95 is removably mounted Within the member 91, with its bottomend resting on the annular disc 94 and with the longitudinal open end ofthe container aligned with the opening in the disc.

The tubular member 91 has a tapered side wall for a purpose hereinafterto be described and is provided with upper and lower circular openings96 in which are secured, as by welding, the nozzles 81 to which theupper and lower flexible pipes 38 and 39 are secured.

A baille member 97 is mounted in the space between the bottom of themember 91 and the annular disc 94, and an upper baille member 98 issecured to the underside of the cover plate 93 and is removabletherewith. The upper and lower baille members 98 and 97 are identical inconstruction and, as shown in Fig. 10, each comprises a generallyelliptical-shaped flat sheet 99 extending upwardly (downwardly) from thebottom (top) of the member 91 to insure an even ow of iluid through themember 91; a side wall forming member 100; and insulating material 101placed within the pocket formed by the members 99 and 100 and the bottom(top) wall of the member 91 (see Fig. l0).

The containers 95 are identical in construction and, as shown in Figs.lO and 11, each comprises two concentric tubular screens 102, 103, heldin spaced-apart relation by a plurality of longitudinal radial fins 104,with the annular space between the screens closed at the bottom, as by aflanged annular plate 105. The mesh of the screens is such as to retaina granular adsorbent material 106 in the annular space between thescreens. In the instant case, the adsorbent material may be of anyadsorbent having characteristics substantially like silica gel or thegel of other activated hydrous oxides. Preferably silica gel is used. l

Each of the containers 95 is closed at its top by means of concentrichoops or metal bands 107, 108 mounted on the concentric screens 102,103, anda cover plate 109 is detachably connected to the inner hoop orband 108, as by screws, and having a depending annular flange 110fitting between the hoops or bands 107, 108. A depending cylindrical lin111 is secured to the flange 110 and projects downwardly between andbelow the hoops or bands 107, 108, and fits in slits 112 formed in theupper ends of the radial fins 104, all as shown in Figs. l0 and ll. Theconstruction is such that, as the silica gel settles down, leaving aspace between the top portion of the wire screens devoid of silica gel,the fin 111 will prevent fluid from passing through the space.

Mounted within the inner wire screen 103 is an ini verted substantially'conically shaped baille member 113. The baille member 113 is closed atits apex which extends downwardly to a point near the bottom of thecontainer and has its upper peripheral edge suitably secured to the band108, as by welding. Preferably, the baille member 113 is made of thinsheet metal.

When the container is mounted within the hollow member 91, as shown inFig. l0, the elongated annular space between the walls of the member 91and the inverted conical baille member 113 forms an elongatedfrusto-conically shaped duct which is annular in cross section. Theannular container, filled with silica gel, is positioned in the ductbetween the members 91 and 113 in such manner thatit forms a barrierextending longitudinally across the duct from top to bottom. The crosssectional areas of the duct at its top and bottom are substantiallyequal and the tapers of its side walls are such that a substantiallyuniform velocity is obtained on both sides of the barrier as fluid istransferred from the upstream to the downstream side, regardless of thedirection of flow, thereby creating a substantially constant static headover the face of the barrier, resulting in av substantially uniformdistribution of the fluid throughout the entire barrier area. Thus, itwill be seen that by using the members 91 and 113, as baffle members,the entire area is made use of with resultant increase in eciency,capacity and economy.

Means may be provided so that the containers 95 which hold the adsorbentmaterial may readily be removed from and replaced in the vessels 31. Asshown,

such means may comprise an opening 114 formed in` the top of the vessel20 having a cylindrical member 115 welded therein and provided with areadily removable closure disc 116 secured in the upper end of themember 115, as by means of a split shear ring 117 bolted thereto andfitted into a circumferential recess 118 formed in the inner surface ofthe member 115, andan 0ring packing 119 mounted between the closure disc116 and the side wall of the member 115 to insure gas tightness.

The flows of the various gases through the various stages of theadsorber and the auxiliary apparatus are schematically shown in Fig. l.

As there shown, the natural gas is supplied under high pressure fromabout 800 p. s. i. to about 1000 p. s. i. by pipe line 6 and entersmanifold a of the upper distributive assemblage through inlet-outletconduit 40. From manifold a the gas passes through openings 74 formed inthe upper tube sheet disc valve 35 and flexible pipes 3S into the upperend portion of the group of vessels 31 which are at that time incommunication with the manifold a. The gas passes down through thesilica gel beds therein into the bottoms of the vessels. The bafflemembers 113, in cooperation with the tapered side walls of the vessels31, insure a substantially uniform flow and distribution of the gasthrough the silica gel beds, which adsorb some of the water vapor andcondensable hydrocarbons from the gas. From the bottoms of the vessels31, the now partially dried gas passes through outlet pipes 39 andopenings 74 in the lower tube sheet disc valve 35 into the manifold a ofthe lower distributive assemblage.

From the lower manifold a of the lower distributive assemblage, the gaspasses through inlet-outlet conduit 40 and pipe line 7 and intercooler 2to the second adsorption stage and enters manifold b of the lowerdistributive assemblage through inlet-outlet conduit 41. From the lowermanifold b the gas passes through openings 74 in the tube sheet discvalve 35 and inlet pipes 39 into the lower end portion of the group ofvessels 31 which are at that time in communication with manifold b. Thegas passes upwardly through the vessels 31 of the second group andthrough the silica gel beds therein into the tops thereof, additionalwater vapor and con densable hydrocarbons being adsorbed from the vgasduring its passage throughthe silica gel beds.

From the' tops of the vessels 3i of the second' adsorption group, thegas passes through pipes 38 and openings 74 in the upper tube sheet discvalve of the upper distributive assemblage into the upper manifold b.

From the upper manifold b the gas passes through inlet-outlet pipe 41and pipe line 8 and intercooler 2 to the third adsorption stage andenters upper manifold c of the upper distributive assemblage throughinlet-outlet conduit 42.

From the upper manifold c the gas passes through openings 74 in the tubesheet disc valve 35 and inlet pipes 38 into the upper end portions ofthe group of vessels 31 which are at that time in communication withmanifold c. The gas passes downwardly through the vessels 31 of thethird group and through the silica gel beds therein into the bottomsthereof, the remaining moisture and condensable hydrocarbon content ofthe gas being adsorbed during its passage through the silica gel beds.

From the bottoms of the vessels 31 of the third group, the gas passesthrough pipes 39 and openings 74 in the tube sheet disc valve 35 intothe lower manifold c. From the lower manifold c the gas passes throughinletoutlet conduit 42' and pipe line 9 to the various points of use.

The removal and recovery of the moisture' and hydrocarbons from the bedsof adsorbent material is effected in the activation stage. Theactivation gas, a captive gas, is heated in a heater 3, where itstemperature is raised to from 300 F. to 600 F., depending upon themoisture content and the type of hydrocarbons to be recovered. From theheater, the heated activation gas passes through pipe line 1d andinlet-outlet conduit 45 into the lower manifold f of the lowerdistributive 'assemblage. From the manifold f the hot activation gaspasses through openings '74 in the lower tube sheet disc valve 35 andtiexible pipes 39 into the lower end portions of the groups of Vessels31 which are at that time in communication with manifold f. The gaspasses upwardly through vessels 31 of the activation group and throughthe silica gel beds therein into the tops thereof. As the hot gas passesthrough the adsorbent material it removes the adsorbed moisture vaporand hydrocarbons therefrom. From the tops of the vessels 31, the hotmoisture, hydrocarbon laden gas passes through flexible pipes 38 andopenings 74 in the lower tube sheet disc valve 35 into the uppermanifold f. From the upper manifold f, the hot gas passes throughinlet-outlet conduit 45 and pipe line 11 to the condenser separator 5where the moisture and condensable hydrocarbons are condensed andseparated. The water and hydrocarbons 'are drained from the separator bya suitable drain line. From the condenser separator 5, the stripped`captive gas passes through pipe line 12 to the blower 4 and is recycledby the blower through pipe line 13 and the heater 3, back through theactivation stage. This recirculation process is continuous.

The captive stream of gas in the activation system is circulated bymeans of lthe blower 4, through the heater 3, the activation stage ofthe adsorber, and the condenser separator 5. The composition of thisstream will build up gradually in terms of condensable vapors, composedchiefly of hydrocarbons, until the dew point of the captive gas streamreaches condenser temperature, and will thereafter yield as liquid allthe condensable vapors desorbed in the activation stage of the adsorber.

ln order to prevent slippage of activation gas, rich in desorbedproducts, into the outgoing stripped gas, and in order to preventdilution of the recycling activation gas, a first purging stage isprovided ahead of and a second and third purging stage are providedfollowing the activation stage.

The effluent gas from the second purging stage, which consists chiefiyof slippage activation gas is used as the purging gas for the rstpurging stage and passes from the second purging stage through pipe line14 and inletoutlet conduit 46 into; the lower manifold g of the lowerdistributive assemblage. From the manifold g the purging gas passesthrough openings '74 in the lower tube sheet disc valve 35 `and iiexiblepipes 39 into the lower portions of the group of vessels 3E which are atthat time in communication with manifold g. The gas passes upwardlythrough the vessels 3l of the first purging stage and through the silicagel beds therein into the tops thereof. As the purging gas passesthrough the adsorbent material it removes the slippage natural gas,thereby purging beds. From the tops of the vessels 3l the etiiuent gasconsisting substantially of slippage gas from the first adsorption stagepasses through flexible pipes 3S and openings 74 in the upper tube sheetdisc valve 35 into the upper manifold g. From the upper manifold ,s thegas passes through inlet-outlet conduit 46 and pipe line i5 to suctionblower it and from blower d passes through pipe line 16 back into pipeline a and joins the natural gas being treated on its way to theadsorber.

The gas used as the purging gas in the second purging stage is obtainedby continuously diverting a portion of the flow or the stripped naturalgas through pipe line 9 from the last adsorption stage of the adsorberthrough pipe line 17 and inlet-outlet conduit fifi into the lowermanifold e of the lower distributive assemblage. From the manifold e thepurging gas passes through openings 74 in the lower tube sheet discvalve 35 and tiexible pipes 39 into the lower end portions of the groupof vessels 3i which are at that time in communication with manifold e.The gas passes upwardly through the vessels 31 of the second purginggroup and through the silica gel beds therein into the tops thereof. Asthe purging gas passes through the adsorbent material it removes anyremaining activation gas or deposited vapors therefrom, thereby purgingthe beds. From the tops of the vessels 31, the eiiiuent gas consistingsubstantially of slippage activation gas passes through tiexible pipes38 and openings 74 in the upper tube sheet disc valve 35 into the uppermanifold e. From the `upper manifold e the gas passes throughinletoutlet `conduit 44 and pipe line 14 to the first purging stage ofthe adsorber.

A portion of the purging gas flowing through pipe line 17 is divertedland passes through pipe line 17 and inletoutlet conduit 43 into manifoldd of the lower distributive assemblage. From the manifold d the purginggas passes through openings 74 in the tube sheet disc valve 35 and inletpipe 39 into the lower end portion of the group of vessels 31 which areat that time in communication with manifold d. The gas passes upwardlythrough the vessels 31 of the third purging group and through the silicagel beds therein into the tops thereof. The purging gas removes anyremaining activation gas and purges the silica gel beds during itspassage through the beds of the third purging stage.

From the tops of the vessels 31 of the third purging stage the effluentgas consisting substantially of slippage gas from the second purgingstage passes through outlet pipes 38 and openings 74 in the upper tubesheet disc valve of the upper distributive assemblage into the uppermanifold d. From the manifold d the gas passes through inletoutletconduit 43, pipe line 18, and pipe line 15 to the suction blower 4' andfrom blower 4 passes through pipe line 16 into pipe line 6 to join thegas being treated owing through pipe line 6 on its way to the adsorber.

The gas being treated makes three passes through the adsorber, while theactivating gas and each of the purging gases each make a single passthrough the adsorber. For convenience in description, the stage of theadsorber through which the first adsorption passage of the gas beingtreated is made, is called the first adsorption stage, the stage throughwhich the second ladsorption passage is made is called the secondadsorption stage, the stage through which the third adsorption passageis made is called the third adsorption stage, the stage through whichthe hot gas used for activation passes is called the activation stage,the stage through which the first purging gas passes is called the rstpurging stage, the stage through which the -second purging gas passes iscalled the second purging stage, andthe stage through which the thirdpurging gas passes iscalled the third purging stage. Also, the vessels31 are called zones in which either adsorption, activation,'or purging4takes place, depending upon the particular uid flowing therethrough ata given time. In addition, the condenser separator 5 is called acondensing and separating zone or stage.

In the particular embodiment of the invention illustrated, the valvediscs 35 and the vessels 31 are rotated clockwise, as viewed in Fig. 2,and at a rate such that the euent gas flow from the purging stages willbe substantially volumetric with the slippage gas brought into thesestages as the vessels 31 are rotated; thus it will be seen that, as thevalves 35 and the vessel 31 rotate, each of the vessels 31 will besuccessively brought in into communication with the manifolds g, f, e,d, c, b and a in the upper and lower distributive assemblages, so thateach vessel 31 will, in turn, become ar first purging zone, anactivation zone, a second purging zone, a third purging zone, a thirdadsorption zone, a second adsorption zone, and a first adsorption zone.A

Suitable stop valves are provided at any desired point in any pipelineto provide means for controlling the ow of the various mediums throughthe various stages of the adsorber andthe auxiliary apparatus.

Also in order to prevent any undue build up of pressure within theactivation stage, a controlled portion of the recycling captiveactivation gas may be diverted through pipe line 19 into the ow Vof thepurging gas passing through pipe line 14 into the first purging stage. v

From the foregoing, it readily will be seen that there has been provideda novel and improved cyclic adsorption process forremoving'andrecovering moisture and condensable hydrocarbons from wet natural gas inwhich aplurality of purging steps are employed so as to permit abuild upof desorbed products in the recycling captive activation `gas stream bypreventing the dilution of the activation ygas by slippage gas and alsoto prevent loss of desorbed products by slippage of the activation gasinto the outgoing eliluent stripped fluid.

While some of the flows of uid through the apparatus have been describedas entering the top distributive assemblage and owing downward to andout of the bottom distributive assemblage, obviously, the ilows may bein either direction.

Obviously, too, the present invention is not restricted to theparticular embodiments thereof herein shown and described.

What is claimed is:

1. In the process of treating wet natural ygas to remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent material with the gas to be treated with resultantadsorption of the water vapor and condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and remove the Water andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor further contact with the gas to be treated, the improvement whichcomprises rotating a series of separated beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a first purging stage, an activation stage, a second purgingstage, and at least one adsorption stage; continuously directing a flowof the gas to be treated under high pressure and in succession throughthe adsorption stages so that the water vapor and condensablehydrocarbon content thereof which is to be removed will be adsorbed bythe adsorbent material therein; continuously heating and recycling a owof activation medium through said activation `stage to desorb the waterand condensable hydrocarbons contained in the beds of adsorbent materialtherein and reactivate the adsorbent material; continuously directingthe ow of the effluent gas from the second purging stage through thefirst purging stage to remove all ofthe gas being treated therefrom;vcontinuously directing the ow of the effluent gas from the first purgingstage into the flow of the gas being treated on its way to the irstadsorption stage; continuously diverting a portion of the ow oftheeflluent stripped gas being treated from the last of the adsorptionstages and directing its ow through the second purging stage to removeall ofthe activation medium therefrom; and continuously directing the owof the captive activation medium as it is recycled and after its passagethrough the activation stage, through a condensing and separating stageand there condensing and removing the water and condensable hydrocarbonstherefrom.

2. In the process of treating wet natural gasto remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent material with the gas to be treated with resultantadsorption of the water vapor and the condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and remove the water vapor andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor,

further contact with the gas to be treated, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a flow of acaptive activation medium under high pressure through at least one ofsaid zones to desorb the water and condensable hydrocarbons contained inthe beds of adsorbent material therein and reactivate the adsorbentmaterial; continuously` directing a first flow of a purging medium underhigh pressure through at least another one of said zones to purge thezone; continuously directing a second ow' of a purging medium under highpressure through at least another one of said zones to purge the zone;continuously directing the flow of the gas being treated under highpressure through the remainder of said Zones so that' the water vaporandy some of the hydrocarbon ticular adsorbent material and theparticular flow of uid in each of said Zones so that each zone becomesin succession a rst purging zone, an activation zone, a second purgingzone and an adsorption Zone; continuously directing the flow of theeffluent gas from the second purging zone into the first purging zonefor use as the first purging medium and continuously directing the ow ofthe eluent -gas from the lirst purging zone back into the flow of thegas being treated on its way to the first adsorption zone; continuouslydiverting a portion of the stripped eliuent gas from the last adsorptionzone for use as the second purging medium; and continuously directingthe flow of the captive activation medium as it is recycled and afterits passage through the activation zone, through a condensing andseparating zone and there condensing and removing the water andcondensable hydrocarbons therefrom.

3. In the process of treating Wet natural gas to remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent material with the gas to be treated with resultantadsorption of the water vapor and condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and remove the water andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor further contact with the gas to be treated, the improvement whichcomprises rotating a series of separated beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a rst purging stage, an activation stage, a second purgingstage, a third purging stage, and a plurality of adsorption stages;`continuously directing a ow of the gas to be treated under high pressurein succession through said adsorption stages so that the water vapor andthe condensable hydrocarbon content thereof which is to be removed willbe adsorbed by content of the. gas will be adsorbed by the adsorbentmaterial therein;A periodically shifting therelative positions of thepar-v the adsorbent material as it passes through said adsorptionstages; continuously heating and recycling a flow of activation mediumthrough said activation stage to desorb the Water and condensablehydrocarbons contained in the beds of adsorbent material therein andreactivate the adsorbent material; continuously directing the flow ofthe eluent gas from the second purging stage through the rst purgingstage to remove all of the gas being treated therefrom and continuouslydirecting the flow of the efiluent gas from the first purging stage intothe ow of the gas being treated on its Way to the first adsorptionstage; continuously diverting a portion of the flow of the effluentstripped gas being treated from the last adsorption stage and directingits flow through the second and third purging stages; continuouslydirecting the How of the eliuent gas from the third purging stage intothe flow of the gas being treated on its way to the first adsorptionstage and continuously directing the iiow of the captive activationmedium as it is recycled and after its passage through the activationstage, through a condensing and separating stage and there condensingand removing the Water and condensable hydrocarbons therefrom.

4. In the process of treating wet natural gas to remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent material with the gas to be treated with resultantadsorption of the water vapor and condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and remove the water andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor further contact with the gas to be treated, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a flow of acaptive activation medium under high pressure through at least one ofsaid zones to desorb the water and condensable hydrocarbons contained inthe beds of adsorbent material therein; continuously directing a rstflow of a purging medium u nder high pressure through at least anotherone of said zones to purge the zone; continuously directing a second owof a purging medium under high pressure through at least another one ofsaid zones to purge the zone; continuously directing a third ow of apurging medium under high pressure through at least another one of saidzones to purge the zone; continuously directing the flow of the gasbeing treated under high pressure through the remainder of said zones sothat the water vapor and some of the condensable hydrocarbon content ofthe gas will be adsorbed by the adsorbent material` therein,periodically shifting the relative positions of the particular adsorbentmaterial and particular flow of fluid in each of said zones so that eachzone becomes in succession a rst purging zone, an activation zone, asecond purging zone, a third purging zone, and an adsorption zone;continuously directing the ilow of the effluent uid from the secondpurging zone into the first purging zone for use as the lirst purgingmedium and continuously directing the flow of the eiuent huid from thefirst purging zone back into the ow of the gas being treated on its Wayto the Iirst adsorption zone; continuously diverting a portion of thestripped etiluent gas from the last adsorption zone for use as thesecond and third purging mediums; continuously directing the tlow ofthel eluent fluid from the third purging zone into the flow of the gasbeing treated on its Way to the first adsorption zone; and continuouslydirecting the ow of the captive activation medium as it is recycled andafter its passage through the activation zone, through a condensing andseparating zone and there condensing and removing the Water andcondensable hydrocarbons therefrom.

References Cited in the tile of this patent UNITED STATES PATENTS1,721,033 Okochi July 16, 1929 1,998,774 Bulkeley Apr. 23, 19352,507,608 Miller May 16, 1950

1. IN THE PROCESS OF TREATING WET NATURAL GAS TO REMOVE AND/OR RECOVERWATER VAPOR AND CONDENSABLE HYDROCARBONS THEREFROM INVOLVING THE CONTACTOF ADSORBENT MATERIAL WITH THE GAS TO BE TREATED WITH RESULTANTADSORPTION OF THE WATER VAPOR AND CONDENSABLE HYDROCARBONS BY THEADSORBENT MATERIAL AND THE SUBSEQUENT TREATMENT OF THE ADSORBENTMATERIAL WITH A HEATED MEDIUM TO VAPORIZE AND REMOVE THE WATER ANDCONDENSABLE HYDROCARBONS AND THEREBY REACTIVATE THE ADSORBENT MATERIALFOR FURTHER CONTACT WITH THE GAS TO BE TREATED, THE IMPROVEMENT WHICHCOMPRISES ROTATING A SERIES OF SEPARATED BEDS OF ADSORBENT MATERIALDIRECTLY IN SUCCESSION AND SUBSTANTIALLY CONTINUOUSLY RELATIVE TO ANDTHROUGH A FIRST PURGING STAGE, AN ACTIVATION STAGE, A SECOND PURGINGSTAGE, AND AT LEAST ONE ADSORPTION STAGE; CONTINUOUSLY DIRECTING A FLOWOF THE GAS TO BE TREATED UNDER HIGH PRESSURE AND IN SUCCESSION THROUGHTHE ADSORPTION STAGES SO THAT THE WATER VAPOR AND CONDENSABLEHYDROCARBON CONTENT THEREOF WHICH IS TO BE REMOVED WILL BE ADSORBED BYTHE ADSORBENT MATERIAL THEREIN; CONTINUOUSLY HEATING AND RECYCLING AFLOW OF ACTIVATION MEDIUM THROUGH SAID ACTIVATION STAGE TO DESORB THEWATER AND CONDENSABLE HYDROCARBONS CONTAINED IN THE BEDS OF ADSORBENTMATERIAL THEREIN AND REACTIVATE THE ADSORBENT MATERIAL; CONTINUOUSLYDIRECTING THE FLOW OF THE EFFUENT GAS FROM THE SECOND PURGING STAGETHROUGH THE FIRST PURGING STAGE TO REMOVE ALL OF THE GAS BEING TREATEDTHEREFROM; CONTINUOUSLY DIRECTING THE FLOW OF THE EFFUENT GAS FROM THEFIRST PURGING STAGE INTO THE FLOW OF THE GAS BEING TREATED ON ITS WAY TOTHE FIRST ADSORPTION STAGE; CONTINUOUSLY DIVERTING A PORTION OF THE FLOWOF THE EFFUENT STRIPPED GAS BEING TREATED FROM THE LAST OF THEADSORPTION STAGES AND DIRECTING ITS FLOW THROUGH THE SECOND PURGINGSTAGE TO REMOVE ALL OF THE ACTIVATION MEDIUM THEREFROM; AND CONTINUOUSLYDIRECTING THE FLOW OF THE CAPTIVE ACTIVATION MEDIUM AS IT IS RECYCLEDAND AFTER ITS PASSAGE THROUGH THE ACTIVATION STAGE, THROUGH A CONDENSINGAND SEPARATING STAGE AND THERE CONDENSING AND REMOVING THE WATER ANDCONDENSABLE HYDROCARBONS THEREFROM.